AU2022385699A1 - Carbon dioxide recovery system - Google Patents
Carbon dioxide recovery system Download PDFInfo
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- AU2022385699A1 AU2022385699A1 AU2022385699A AU2022385699A AU2022385699A1 AU 2022385699 A1 AU2022385699 A1 AU 2022385699A1 AU 2022385699 A AU2022385699 A AU 2022385699A AU 2022385699 A AU2022385699 A AU 2022385699A AU 2022385699 A1 AU2022385699 A1 AU 2022385699A1
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- distillation column
- fluid
- carbon dioxide
- reboiler
- absorption liquid
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- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 title claims abstract description 206
- 239000001569 carbon dioxide Substances 0.000 title claims abstract description 103
- 229910002092 carbon dioxide Inorganic materials 0.000 title claims abstract description 103
- 238000011084 recovery Methods 0.000 title claims abstract description 81
- 238000004821 distillation Methods 0.000 claims abstract description 150
- 239000007788 liquid Substances 0.000 claims abstract description 135
- 238000010521 absorption reaction Methods 0.000 claims abstract description 118
- 239000012530 fluid Substances 0.000 claims abstract description 89
- OKKJLVBELUTLKV-UHFFFAOYSA-N Methanol Chemical compound OC OKKJLVBELUTLKV-UHFFFAOYSA-N 0.000 claims description 255
- 239000007789 gas Substances 0.000 claims description 75
- 239000012809 cooling fluid Substances 0.000 claims description 21
- 238000010438 heat treatment Methods 0.000 claims description 18
- 238000001816 cooling Methods 0.000 claims description 10
- 239000004215 Carbon black (E152) Substances 0.000 claims description 6
- 229930195733 hydrocarbon Natural products 0.000 claims description 6
- 150000002430 hydrocarbons Chemical class 0.000 claims description 6
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 4
- 125000004430 oxygen atom Chemical group O* 0.000 claims description 3
- 230000000704 physical effect Effects 0.000 claims description 3
- 238000010992 reflux Methods 0.000 description 16
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 description 11
- 229910052799 carbon Inorganic materials 0.000 description 11
- 230000001105 regulatory effect Effects 0.000 description 9
- 230000006835 compression Effects 0.000 description 6
- 238000007906 compression Methods 0.000 description 6
- 238000004088 simulation Methods 0.000 description 5
- 239000000126 substance Substances 0.000 description 5
- 238000010586 diagram Methods 0.000 description 4
- CSCPPACGZOOCGX-UHFFFAOYSA-N Acetone Chemical compound CC(C)=O CSCPPACGZOOCGX-UHFFFAOYSA-N 0.000 description 3
- LFQSCWFLJHTTHZ-UHFFFAOYSA-N Ethanol Chemical compound CCO LFQSCWFLJHTTHZ-UHFFFAOYSA-N 0.000 description 3
- KFZMGEQAYNKOFK-UHFFFAOYSA-N Isopropanol Chemical compound CC(C)O KFZMGEQAYNKOFK-UHFFFAOYSA-N 0.000 description 3
- 238000009835 boiling Methods 0.000 description 3
- 239000000470 constituent Substances 0.000 description 3
- 238000005265 energy consumption Methods 0.000 description 3
- VLKZOEOYAKHREP-UHFFFAOYSA-N n-Hexane Chemical compound CCCCCC VLKZOEOYAKHREP-UHFFFAOYSA-N 0.000 description 3
- 230000007423 decrease Effects 0.000 description 2
- 150000001336 alkenes Chemical class 0.000 description 1
- 238000009833 condensation Methods 0.000 description 1
- 230000005494 condensation Effects 0.000 description 1
- 230000003247 decreasing effect Effects 0.000 description 1
- IEJIGPNLZYLLBP-UHFFFAOYSA-N dimethyl carbonate Chemical compound COC(=O)OC IEJIGPNLZYLLBP-UHFFFAOYSA-N 0.000 description 1
- 238000007599 discharging Methods 0.000 description 1
- 230000000694 effects Effects 0.000 description 1
- 239000000203 mixture Substances 0.000 description 1
- 238000012986 modification Methods 0.000 description 1
- 230000004048 modification Effects 0.000 description 1
- 238000010248 power generation Methods 0.000 description 1
- 238000010791 quenching Methods 0.000 description 1
- 230000000171 quenching effect Effects 0.000 description 1
- 239000002994 raw material Substances 0.000 description 1
- 238000007670 refining Methods 0.000 description 1
- 239000007921 spray Substances 0.000 description 1
- 238000011144 upstream manufacturing Methods 0.000 description 1
Classifications
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/46—Removing components of defined structure
- B01D53/62—Carbon oxides
-
- B—PERFORMING OPERATIONS; TRANSPORTING
- B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
- B01D—SEPARATION
- B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
- B01D53/34—Chemical or biological purification of waste gases
- B01D53/96—Regeneration, reactivation or recycling of reactants
-
- C—CHEMISTRY; METALLURGY
- C01—INORGANIC CHEMISTRY
- C01B—NON-METALLIC ELEMENTS; COMPOUNDS THEREOF; METALLOIDS OR COMPOUNDS THEREOF NOT COVERED BY SUBCLASS C01C
- C01B32/00—Carbon; Compounds thereof
- C01B32/50—Carbon dioxide
-
- C—CHEMISTRY; METALLURGY
- C07—ORGANIC CHEMISTRY
- C07C—ACYCLIC OR CARBOCYCLIC COMPOUNDS
- C07C31/00—Saturated compounds having hydroxy or O-metal groups bound to acyclic carbon atoms
- C07C31/02—Monohydroxylic acyclic alcohols
- C07C31/04—Methanol
-
- Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
- Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
- Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
- Y02C20/00—Capture or disposal of greenhouse gases
- Y02C20/40—Capture or disposal of greenhouse gases of CO2
Landscapes
- Chemical & Material Sciences (AREA)
- Engineering & Computer Science (AREA)
- Organic Chemistry (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Oil, Petroleum & Natural Gas (AREA)
- General Chemical & Material Sciences (AREA)
- Analytical Chemistry (AREA)
- Biomedical Technology (AREA)
- Health & Medical Sciences (AREA)
- Environmental & Geological Engineering (AREA)
- Sustainable Development (AREA)
- Life Sciences & Earth Sciences (AREA)
- Inorganic Chemistry (AREA)
- Gas Separation By Absorption (AREA)
- Carbon And Carbon Compounds (AREA)
- Treating Waste Gases (AREA)
Abstract
A carbon dioxide recovery system including a first distillation tower, in which an absorption liquid containing absorbed carbon dioxide is heated and thereby caused to release the carbon dioxide, a first reboiler, in which some of the absorption liquid drawn out of the first distillation tower is heat-exchanged with steam, a second reboiler, in which some of the absorption liquid drawn out of the first distillation tower is heat-exchanged with a fluid which is neither an effluent gas from the first distillation tower nor steam, and a first compressor, whereby the fluid is compressed before flowing into the second reboiler.
Description
[0001] The present disclosure relates to a carbon dioxide recovery system.
The present application claims priority based on Japanese Patent Application No. 2021
184701 filed on November 12, 2021, the entire content of which is incorporated herein by
reference.
[0002] Patent Document 1 describes a carbon dioxide recovery system equipped with an
absorption column in which carbon dioxide is absorbed into an absorption liquid by bringing
gas containing carbon dioxide into gas-liquid contact with the absorption liquid, and a
distillation column in which carbon dioxide is released from the absorption liquid that has
absorbed carbon dioxide in the absorption tower. This distillation column is provided with a
reboiler for heating the absorption liquid in the distillation column. Multiple reboilers may be
provided, for example, a reboiler for heating the absorption liquid by heat exchange between
the absorption liquid and steam, and a reboiler for heating the absorption liquid by heat
exchange between the absorption liquid and steam flowing out of the distillation column and
then pressurized by a compressor. With this configuration, not only steam but also heat of
steam flowing out of the top of the distillation column and then compressed by a compressor is
used as a heat source to heat the absorption liquid, so that the amount of steam used is reduced,
and the amount of external heat supply can be reduced.
Citation List
Patent Literature
[0003] Patent Document 1: JP6064771B
Problems to be Solved
[0004] However, since carbon dioxide recovery systems are usually installed as part of a
producing plant of any substance, power generation plant, or the like, it is conceivable that there
may be a more suitable heat source for heating the absorption liquid in the distillation column,
and if such a suitable heat source is used, the amount of external heat supply could be further
reduced.
[0005] In view of the above, an object of at least one embodiment of the present disclosure
is to provide a carbon dioxide recovery system with a reduced amount of external heat supply
to the distillation column for releasing carbon dioxide from an absorption liquid that has
absorbed carbon dioxide.
Solution to the Problems
[0006] In order to achieve the above-described object, a carbon dioxide recovery system
according to the present disclosure is equipped with: a first distillation column for heating an
absorption liquid that has absorbed carbon dioxide to release carbon dioxide from the
absorption liquid; a first reboiler for exchanging heat between the absorption liquid extracted
from the first distillation column and steam; a second reboiler for exchanging heat between the
absorption liquid extracted from the first distillation column and a fluid different from both an
effluent gas from the first distillation column and the steam; and a first compressor for
compressing the fluid before the fluid flows into the second reboiler.
Advantageous Effects
[0007] With the carbon dioxide recovery system of the present disclosure, in the first
reboiler, the absorption liquid is heated by heat exchange between the absorption liquid and
steam, and in the second reboiler, the absorption liquid is heated by heat exchange between the
absorption liquid and a fluid different from both the effluent gas from the first distillation
column and the steam after the fluid is compressed, so that the amount of steam used is reduced,
-91)- and the amount of external heat supply to the first distillation column can be reduced.
[0008] FIG. 1 is a schematic configuration diagram of a carbon dioxide recovery system
according to the first embodiment of the present disclosure.
FIG. 2 is a schematic configuration diagram of a carbon dioxide recovery system
according to the second embodiment of the present disclosure.
FIG. 3 is a schematic configuration diagram of a carbon dioxide recovery system
according to the third embodiment of the present disclosure.
FIG. 4 is a schematic configuration diagram of a carbon dioxide recovery system
according to the fourth embodiment of the present disclosure.
[0009] Hereinafter, a carbon dioxide recovery system according to embodiments of the
present disclosure will be described with reference to the drawings. The embodiment to be
described below indicates one aspect of the present disclosure, does not intend to limit the
disclosure, and can optionally be modified within a range of a technical idea of the present
disclosure.
[0010] (First Embodiment)
<Configuration of carbon dioxide recovery system according to first embodiment of present
disclosure>
As shown in FIG. 1, a carbon dioxide recovery system 1 according to the first embodiment
of the present disclosure will be described using a configuration example in which the system
is provided in a methanol producing plant. The carbon dioxide recovery system 1 is equipped
with a first distillation column 2 and a second distillation column 10. The first distillation
column 2 communicates through an absorption liquid supply line 3 with an absorption column
(not shown) for absorption of carbon dioxide into an absorption liquid by bringing gas
containing carbon dioxide into gas-liquid contact with the absorption liquid, for example.
[0011] The first distillation column 2 is provided with a circulation line 4 for circulating
the absorption liquid so that the absorption liquid in the first distillation column 2 is extracted
from the bottom of the first distillation column 2 and returned into the first distillation column
2. The circulation line 4 includes a first line portion 4a and a second line portion 4b where the
flow of the absorption liquid is divided into two parts and flows parallel to each other. The
first line portion 4a and the second line portion 4b are provided with a first reboiler 5a and a
second reboiler 5b, respectively. In other words, the first reboiler 5a and the second reboiler
5b are provided in parallel with each other with respect to the flow direction of the absorption
liquid. The first reboiler 5a is a heat exchanger for heat exchange between the absorption
liquid flowing in the first line portion 4a and steam to heat the absorption liquid. The second
reboiler 5b is a heat exchanger for heat exchange between the absorption liquid flowing in the
second line portion 4b and a fluid different from the steam to heat the absorption liquid.
Illustrative examples of the fluid in the first embodiment will be described later.
[0012] The first distillation column 2 is also provided with a condensing device 6 which
returns a condensate obtained by cooling a gas that flows out of the top of the first distillation
column 2 (hereinafter referred to as "effluent gas") to the first distillation column 2. The
condensing device 6 includes an effluent gas line 6a through which the effluent gas flows, a
cooler 6b disposed in the effluent gas line 6a, a reflux tank 6c connected to the downstream end
of the effluent gas line 6a, and a condensate line 6d through which the condensate in the reflux
tank 6c is returned to the first distillation column 2. The cooler 6b can be, as an example, a
heat exchanger for heat exchange between the effluent gas and any cooling fluid to cool the
effluent gas. In addition to the condensate, there is a gas in the reflux tank 6c, which is mainly
carbon dioxide. The top of the reflux tank 6c may be connected to one end of a line connected
to a device that uses carbon dioxide, in the case of thefirst embodiment, for example, one end
of a feedstock supply line 7 for supplying carbon dioxide as feedstock to a methanol producing
plant.
[0013] The second distillation column 10 is not limited to a particular configuration as long
as it is different from the first distillation column 2, but in the first embodiment, the second distillation column 10 is described as a distillation column for obtaining a fluid with a higher methanol concentration by distillation of a crude fluid mainly composed of methanol
(hereinafter referred to as "crude methanol fluid") in a methanol producing plant. The second
distillation column 10 communicates through a crude fluid supply line 16 with a device (not
shown) for producing crude methanol fluid.
[0014] Similarly to the first distillation column 2, the second distillation column 10 is
provided with a reboiler 11 for heating the crude methanol fluid in the second distillation
column 10 and a condensing device 12 for condensing methanol vapor that flows out of the top
of the second distillation column 10. The reboiler 11 is, for example, a heat exchanger for
heat exchange between steam and the crude methanol fluid. The condensing device 12
includes, for example, a cooler 12a, which is a heat exchanger for heat exchange between the
methanol vapor that flows out of the second distillation column 10 and any cooling fluid, a
reflux tank 12b into which the fluid (mainly liquid methanol) cooled by the cooler 12a flows, a
return line 12c for returning part of the liquid methanol in the reflux tank 12b to the second
distillation column 10, and a methanol supply line 12d for supplying the remaining liquid
methanol in the reflux tank 12b as a product.
[0015] One end of a line 13 through which the methanol vapor discharged from the second
distillation column 10 flows is connected to the top of the second distillation column 10, and
the other end of the line 13 is connected to the reflux tank 12b of the condensing device 12.
The line 13 is designed to pass through the second reboiler 5b, i.e., to exchange heat between
the absorption liquid flowing in the second line portion 4b and the methanol vapor flowing in
the line 13 in the second reboiler 5b. Therefore, in the first embodiment, the above-described
fluid is the methanol vapor that flows out of the top of the second distillation column 10. The
line 13 is provided with a first compressor 14 between the second distillation column 10 and
the second reboiler 5b, and a regulating valve 15 for regulating the pressure between the second
reboiler 5b and the condensing device 12.
[0016] <Operation of carbon dioxide recovery system according to first embodiment of
present disclosure>
Next, the operation of the carbon dioxide recovery system 1 according to the first
embodiment of the present disclosure will be described. The absorption liquid that has
absorbed carbon dioxide flows into the first distillation column 2 through the absorption liquid
supply line 3. The absorption liquid in the first distillation column 2 circulates so that it is
extracted from the bottom of the first distillation column 2 and then returned into the first
distillation column 2. During circulation of the absorption liquid, the absorption liquid
flowing in the first line portion 4a and the second line portion 4b are heated in thefirst reboiler
5a and the second reboiler 5b, respectively.
[0017] When the temperature of the absorption liquid rises due to heating of the absorption
liquid in each of the first reboiler 5a and the second reboiler 5b, carbon dioxide absorbed in the
absorption liquid is removed from the absorption liquid. Carbon dioxide and other gas
components removed from the absorption liquid rise in the first distillation column 2 and flow
out of the top of thefirst distillation column 2, then flows through the effluent gas line 6a as the
effluent gas. During flow of the effluent gas through the effluent gas line 6a, the effluent gas
is cooled by the cooler 6b. When the effluent gas is cooled to a lower temperature,
components with low boiling points in the effluent gas condense while most of carbon dioxide
remains a gas. When the cooled effluent gas flows into the reflux tank 6c, the effluent gas is
separated into gaseous and liquid components. The gaseous component, which is mainly
carbon dioxide, is supplied as feedstock to a carbon dioxide consumption device (not shown)
through the feedstock supply line 7. On the other hand, the liquid component is returned to
the first distillation column 2 through the condensate line 6d.
[0018] Meanwhile, the crude methanol fluid that flows into the second distillation column
10 through the crude fluid supply line 16 is heated by the reboiler 11 to a higher temperature.
When the temperature of the crude methanol fluid rises, most of methanol with low boiling
point vaporizes and rises in the second distillation column 10, while most of components with
high boiling points (mainly water) remain a liquid in the second distillation column 10. Vapor
mainly composed of methanol (hereinafter referred to as "methanol vapor") that rises in the
second distillation column 10 and flows out of the second distillation column 10 flows through the line 13.
[0019] The methanol vapor flowing through the line 13 is compressed by the first
compressor 14. Compression by the first compressor 14 raises the temperature of the
methanol vapor. The methanol vapor compressed by the first compressor 14 exchanges heat
with the absorption liquid in the second reboiler 5b and lowers its temperature. Depending on
the temperature, at least part of methanol can condense. The methanol vapor that has
exchanged heat with the absorption liquid in the second reboiler 5b flows through the line 13
as methanol vapor or at least containing liquid methanol, and in the condensing device 12, it is
cooled by the cooler 12a and then flows into the reflux tank 12b. Part of the condensate (liquid
methanol) in the reflux tank 12b is returned to the second distillation column 10 through the
return line 12c, while the remaining condensate is supplied to a device (not shown) for methanol
consumption or storage through the methanol supply line 12d.
[0020] When the methanol vapor flowing through the line 13 is used as a heating medium,
by compressing the heating medium to a higher temperature and using it for heat exchange in
the second reboiler 5b, the latent heat of condensation can also be given to the absorption liquid.
This allows the line 13 and the device associated with the line 13 to operate as a heat pump,
which reduces the overall energy consumption of the carbon dioxide recovery system 1.
[0021] The characteristics of fluid in each device and each line of the carbon dioxide
recovery system 1 and the energy consumed by each device were simulated under conditions
where the amount of carbon dioxide recovered in the first distillation column 2 is 3 t/day, the
amount of methanol supplied as a product from the second distillation column 10 is 2 t/day, and
all methanol vapor that has exchanged heat with the absorption liquid in the second reboiler 5b
condenses into liquid methanol. According to the simulation results, the amount of steam used
in the first reboiler 5a can be reduced by 40 to 50% compared to the case where the absorption
liquid is heated only in the first reboiler 5a.
[0022] Thus, in the first reboiler, the absorption liquid is heated by heat exchange between
the absorption liquid and steam, and in the second reboiler, the absorption liquid is heated by
heat exchange between the absorption liquid and the fluid that flows out of the second distillation column 10 after the fluid is compressed, so that the amount of steam used is reduced.
[0023] (Second Embodiment)
Next, the carbon dioxide recovery system according to the second embodiment will be
described. The carbon dioxide recovery system according to the second embodiment is
modified from the first embodiment so that the fluid that has exchanged heat with the absorption
liquid in the second reboiler 5b is used as a cooling fluid for cooling the effluent gas from the
first distillation column 2 in the condensing device 6. In the second embodiment, the same
constituent elements as those in the first embodiment are associated with the same reference
signs and not described again in detail.
[0024] <Configuration of carbon dioxide recovery system according to second embodiment
of present disclosure>
As shown in FIG. 2, in the carbon dioxide recovery system 1 according to the second
embodiment, the condensing device 6 is provided with a cooler 6e disposed in the effluent gas
line 6a upstream of the cooler 6b. The system is provided with a bypass line 20 connected at
one end to the line 13 between the second reboiler 5b and the regulating valve 15 and connected
at the other end to the line 13 between thefirst compressor 14 and the second distillation column
10. The bypass line 20 is configured to pass through the cooler 6e, i.e., to exchange heat
between the effluent gas flowing in the effluent gas line 6a and a fluid flowing in the bypass
line 20 in the cooler 6e. The bypass line 20 is provided with a regulating valve 21 for
regulating the pressure between the second reboiler 5b and the cooler 6e. The configuration
is otherwise the same as that of thefirst embodiment.
[0025] <Operation of carbon dioxide recovery system according to second embodiment of
present disclosure>
Next, the operation of the carbon dioxide recovery system 1 according to the second
embodiment of the present disclosure will be described. The operation of removing carbon
dioxide from the absorption liquid in the first distillation column 2 and the operation of
generating methanol vapor from the crude methanol fluid in the second distillation column 10
are the same as in the first embodiment. In the second embodiment, the fluid that has exchanged heat with the absorption liquid in the second reboiler 5b becomes a fluid in the state of methanol vapor or at least partially condensed methanol and flows through the bypass line
20 into the cooler 6e. This fluid cools the effluent gas by exchanging heat with the effluent
gas in the cooler 6e. If this fluid contains at least liquid methanol, the liquid methanol
vaporizes through heat exchange with the effluent gas. The methanol vapor flowing out of the
cooler 6e flows into the line 13 between the second distillation column 10 and the first
compressor 14 through the bypass line 20, where it is mixed with the methanol vapor flowing
in the line 13 and compressed by the first compressor 14. The operation is otherwise the same
as that of the first embodiment.
[0026] Thus, since part of the fluid after heat exchange with the absorption liquid in the
second reboiler 5b is used to cool the effluent gas from the first distillation column 2, the
thermal efficiency of the entire carbon dioxide recovery system 1 can be improved. Further, since the cooling fluid after heat exchange with the effluent gas in the cooler 6e is supplied to
the second reboiler 5b after it is mixed with the fluid from the top of the second distillation
column 10 and compressed by the first compressor 14, the thermal efficiency of the entire
carbon dioxide recovery system 1 can be improved.
[0027] In the second embodiment, as in the first embodiment, the characteristics of fluid in
each device and each line of the carbon dioxide recovery system 1 and the energy consumed by
each device were simulated under conditions where the amount of carbon dioxide recovered in
the first distillation column 2 is 3 t/day, the amount of methanol supplied as a product from the
second distillation column 10 is 2 t/day, all methanol vapor that has exchanged heat with the
absorption liquid in the second reboiler 5b condenses into liquid methanol, and all liquid
methanol that has exchanged heat with the effluent gas in the cooler 6e vaporizes. According
to the simulation results, the amount of steam used in the first reboiler 5a can be reduced by 80
to 90% compared to the case where the absorption liquid is heated only in the first reboiler 5a.
[0028] <Modified example of carbon dioxide recovery system according to second
embodiment of present disclosure>
In the second embodiment, the condensing device 6 includes two coolers 6b and 6e, but it may include only the cooler 6e instead of the cooler 6b. Further, the number of coolers 6e is not limited to one, and multiple coolers 6e may be provided in series or in parallel with respect to the flow direction of the effluent gas.
[0029] (Third Embodiment)
Next, the carbon dioxide recovery system according to the third embodiment will be
described. The carbon dioxide recovery system according to the third embodiment is
modified from the second embodiment so that a third reboiler 5c is provided for heating the
absorption liquid in addition to the first reboiler 5a and the second reboiler 5b. In the third
embodiment, the same constituent elements as those in the second embodiment are associated
with the same reference numerals and not described again in detail.
[0030] <Configuration of carbon dioxide recovery system according to third embodiment
of present disclosure>
As shown in FIG. 3, in the carbon dioxide recovery system 1 according to the third
embodiment, the circulation line 4 includes a third line portion 4c provided in parallel with each
of the first line portion 4a and the second line portion 4b. The third line portion 4c is provided
with a third reboiler 5c which exchanges heat between the absorption liquid flowing in the third
line portion 4c and a second fluid to heat the absorption liquid. In other words, the third
reboiler 5c is provided in parallel with each of the first reboiler 5a and the second reboiler 5b
with respect to the flow direction of the absorption liquid. Illustrative examples of the second
fluid in the third embodiment will be described later.
[0031] In the third embodiment, the bypass line 20 is not provided unlike the second
embodiment. Instead, the line 13, one end of which is connected to the top of the second
distillation column 10, is designed to pass through the second reboiler 5b, the cooler 6e, and
then the third reboiler 5c, and the other end of the line 13 is connected to the reflux tank 12b of
the condensing device 12. The line 13 is provided with a second compressor 30 between the
cooler 6e and the third reboiler 5c, and a regulating valve 31 for regulating the pressure between
the third reboiler 5c and the condensing device 12. The configuration is otherwise the same
as that of the second embodiment.
[0032] <Operation of carbon dioxide recovery system according to third embodiment of
present disclosure>
Next, the operation of the carbon dioxide recovery system 1 according to the third
embodiment of the present disclosure will be described. The operation of removing carbon
dioxide from the absorption liquid in the first distillation column 2, the operation of generating
methanol vapor from the crude methanol fluid in the second distillation column 10, and the
operation of exchanging heat between the methanol vapor and the absorption liquid in the
second reboiler 5b and exchanging heat between the methanol vapor and the effluent gas in the
cooler 6e are the same as in the second embodiment. In the third embodiment, the methanol
vapor after heat exchange with the effluent gas in the cooler 6e is compressed by the second
compressor 30. Compression by the second compressor 30 raises the temperature of the
methanol vapor. The methanol vapor compressed by the second compressor 30 exchanges
heat with the absorption liquid in the third reboiler 5c as the second fluid and lowers its
temperature. The second fluid after heat exchange with the absorption liquid in the third
reboiler 5c is supplied to the condensing device 12. The operation of the condensing device
12 is the same as in the second embodiment.
[0033] In the third embodiment, as in the second embodiment, the characteristics of fluid
in each device and each line of the carbon dioxide recovery system 1 and the energy consumed
by each device were simulated under conditions where the amount of carbon dioxide recovered
in the first distillation column 2 is 3 t/day, the amount of methanol supplied from the second
distillation column 10 is 2 t/day, all methanol vapor that has exchanged heat with the absorption
liquid in the second reboiler 5b condenses into liquid methanol, all liquid methanol that has
exchanged heat with the effluent gas in the cooler 6e vaporizes, and all methanol vapor that has
exchanged heat with the absorption liquid in the third reboiler 5c condenses into liquid methanol.
According to the simulation results, the amount of steam used in the first reboiler 5a can be
reduced by 80 to 90% compared to the case where the absorption liquid is heated only in the
first reboiler 5a.
[0034] (Fourth Embodiment)
Next, the carbon dioxide recovery system according to the fourth embodiment will be
described. The carbon dioxide recovery system according to the fourth embodiment is
modified from the first embodiment so that a third reboiler 5c is provided for heating the
absorption liquid in addition to the first reboiler 5a and the second reboiler 5b. In the fourth
embodiment, the same constituent elements as those in the first embodiment are associated with
the same reference signs and not described again in detail.
[0035] <Configuration of carbon dioxide recovery system according to fourth embodiment
of present disclosure>
As shown in FIG. 4, the carbon dioxide recovery system 1 according to the fourth
embodiment is equipped with a third reboiler 5c for heating the absorption liquid in the first
distillation column 2 in addition to the first reboiler 5a and the second reboiler 5b as in the third
embodiment. In the fourth embodiment, the effluent gas line 6a, one end of which is
connected to the top of the first distillation column 2, passes through the third reboiler 5c, and
the other end of the effluent gas line 6a is connected to the reflux tank 6c of the condensing
device 6. The effluent gas line 6a is provided with two third compressors 40a and 40b in series
with each other between the first distillation column 2 and the third reboiler 5c, and a heat
exchanger 41 between the third compressors 40a and 40b for cooling the effluent gas by heat
exchange between the effluent gas and any cooling fluid. The configuration is otherwise the
same as that of thefirst embodiment.
[0036] Although not an essential component of the fourth embodiment, a condensate drain
line 42 may be provided, which is connected at one end to the condensate line 6d and at the
other end to a discharge line 4d, which is a branch of the circulation line 4 to discharge the
absorption liquid out of the system. In this case, regulating valves 43 and 44 for regulating
the flow rates may be provided in the condensate line 6d and the condensate drain line 42 in
order to regulate the amount of condensate returned to the first distillation column 2 and the
amount of condensate flowing in the condensate drain line 42, respectively.
[0037] <Operation of carbon dioxide recovery system according to fourth embodiment of
present disclosure>
Next, the operation of the carbon dioxide recovery system 1 according to the fourth
embodiment of the present disclosure will be described. The operation of removing carbon
dioxide from the absorption liquid in the first distillation column 2, the operation of generating
methanol vapor from the crude methanol fluid in the second distillation column 10, and the
operation of exchanging heat between the absorption liquid and the fluid, methanol vapor, in
the second reboiler 5b and condensing the fluid that has exchanged heat with the absorption
liquid by the condensing device 12 are the same as in the first embodiment. In the fourth
embodiment, the effluent gas from the first distillation column 2 is compressed by each of the
third compressors 40a and 40b while its temperature is adjusted by the heat exchanger 41 as it
flows through the effluent gas line 6a. Compression by each of the third compressors 40a and
40b raises the temperature of the effluent gas. The effluent gas compressed by the third
compressors 40a and 40b exchanges heat with the absorption liquid in the third reboiler 5c as
the second fluid. The effluent gas that has exchanged heat with the absorption liquid in the
third reboiler 5c is treated in the condensing device 6 by the same operation described in the
first embodiment.
[0038] If the condensate drain line 42 is provided, part of the condensate can be discharged
out of the system through the condensate drain line 42 and the discharge line 4d. When part
of the condensate is discharged out of the system, the reflux flow rate of thefirst distillation
column 2 decreases. Decreasing the reflux flow rate of the first distillation column 2 reduces
the reboiler duty in the first distillation column 2. For example, according to simulations by
the inventors of this disclosure, a 50% decrease in the reflux flow rate of the first distillation
column 2 would reduce the reboiler duty in the first distillation column 2 by 10 to 20%.
[0039] In the fourth embodiment, as in the first embodiment, the characteristics of fluid in
each device and each line of the carbon dioxide recovery system 1 and the energy consumed by
each device were simulated under conditions where the amount of carbon dioxide recovered in
the first distillation column 2 is 3 t/day, the amount of methanol supplied as a product from the
second distillation column 10 is 2 t/day, and all methanol vapor that has exchanged heat with
the absorption liquid in the second reboiler 5b condenses into liquid methanol. According to the simulation results, the amount of steam used in the first reboiler 5a can be reduced by 90 to
100% compared to the case where the absorption liquid is heated only in the first reboiler 5a.
[0040] <Modified example of carbon dioxide recovery system according to fourth
embodiment of present disclosure>
In the fourth embodiment, two third compressors 40a and 40b are provided to compress
the effluent gas as the second fluid, but only one third compressor maybe provided. However, by using a multi-stage compressor, the compression ratio per stage can be lowered to reduce
power and improve efficiency. For this reason, the number of third compressors is not limited
to two, but may be three or more. In the fourth embodiment, the heat exchanger 41 is disposed
between the third compressors 40a and 40b, but any device that can cool the gas flowing out of
each compressor can be used. Exemplary alternative means may include a pump configured
to spray liquid into the line where the gas discharged from each compressor flows. The gas
can be cooled by quenching with liquid sprayed from such a pump.
[0041] <Modified example of carbon dioxide recovery system according to each
embodiment>
In the first to fourth embodiments, the second distillation column 10 is a distillation
column for refining methanol in a methanol producing plant, but it is not limited to such a
distillation column, and may be a methanol-derived product producing device, such as devices
for producing dimethyl carbonate from carbon dioxide and methanol, olefins from methanol
(MTO), gasoline from methanol (MTG), etc. Methanol is not limited to that produced in a
plant (product or intermediate), but may be externally procured as a raw material. In this case, instead of the second distillation column 10, which is a distillation column, methanol is supplied
from, for example, a methanol storage facility and a heating device for heating methanol. In
particular, if such a configuration is adopted in the second embodiment, all methanol after heat
exchange with the absorption liquid in the second reboiler 5b may be used as the cooling fluid
in the cooler 6e, and the methanol heated by heat exchange with the effluent gas in the cooler
6e may be supplied back to the second reboiler 5b for heat exchange with the absorption liquid.
Furthermore, in the first to fourth embodiments, the second distillation column 10 is one
- ill - distillation column, but the second distillation column 10 may consist of two or more distillation columns, or it may consist of a combination of one or more distillation columns and a device with a configuration other than a distillation column.
[0042] In the first to fourth embodiments, the fluid used as a heat source in the second
reboiler 5b is methanol vapor, but it is not limited to methanol. Water, or a hydrocarbon with
physical properties of saturation temperature lower than or equal to 100°C at atmospheric
pressure and lower than or equal to 120°C at 10 atmospheres, or a hydrocarbon containing
oxygen atoms may be used as the fluid. Further, the fluid is not limited to pure substances of
such substances, but may contain such substances as part of the fluid. Examples of such
substances include ethanol, acetone, 2-propanol, hexane, and mixtures thereof.
[0043] In the first to fourth embodiments, the first distillation column 2 and the second
distillation column 10 are in the same plant (for example, methanol producing plant), but they
may be in separate plants.
[0044] In the first and second embodiments, the first reboiler 5a and the second reboiler 5b
are installed in parallel with each other with respect to the flow direction of the absorption liquid,
and in the third and fourth embodiments, the third reboiler 5c is installed in parallel with each
of the first reboiler 5a and the second reboiler 5b with respect to the flow direction of the
absorption liquid, but the invention is not limited to these embodiments. The first reboiler 5a
and the second reboiler 5b may be in series with each other, and the third reboiler 5c may be in
series with at least one of the first reboiler 5a and the second reboiler 5b.
[0045] In the first to fourth embodiments and their modifications, the pressure of the second
distillation column 10 may be higher than the pressure of the first distillation column 2. In
this case, the compression ratio in the first compressor 14 can be lowered, so that the overall
energy consumption of the carbon dioxide recovery system 1 can be reduced.
[0046] The contents described in the above embodiments would be understood as follows, for instance.
[0047] [1] A carbon dioxide recovery system according to one aspect is equipped with: a
first distillation column (2) for heating an absorption liquid that has absorbed carbon dioxide to
- 1 s - release carbon dioxide from the absorption liquid; a first reboiler (5a) for exchanging heat between the absorption liquid extracted from the first distillation column (2) and steam; a second reboiler (5b) for exchanging heat between the absorption liquid extracted from the first distillation column (2) and a fluid different from both an effluent gas from the first distillation column (2) and the steam; and afirst compressor (14) for compressing the fluid before the fluid flows into the second reboiler (5b).
[0048] With the carbon dioxide recovery system of the present disclosure, in the first
reboiler, the absorption liquid is heated by heat exchange between the absorption liquid and
steam, and in the second reboiler, the absorption liquid is heated by heat exchange between the
absorption liquid and a fluid different from both the effluent gas from thefirst distillation
column and the steam after the fluid is compressed, so that the amount of steam used is reduced,
and the amount of external heat supply to the first distillation column can be reduced.
[0049] [2] A carbon dioxide recovery system according to another aspect is the carbon
dioxide recovery system of [1], in which the fluid includes water, or a hydrocarbon with
physical properties of saturation temperature lower than or equal to 100°C at atmospheric
pressure and lower than or equal to 120°C at 10 atmospheres, or a hydrocarbon containing
oxygen atoms.
[0050] [3] A carbon dioxide recovery system according to still another aspect is the carbon
dioxide recovery system of [1] or [2], further including a second distillation column (10)
different from the first distillation column (2). The fluid is supplied from the second
distillation column (10).
[0051] With this configuration, in the first reboiler, the absorption liquid is heated by heat
exchange between the absorption liquid and steam, and in the second reboiler, the absorption
liquid is heated by heat exchange between the absorption liquid and the fluid supplied from the
second distillation column after the fluid is compressed, so that the amount of steam used is
reduced, and the amount of external heat supply to the first distillation column can be reduced.
[0052] [4] A carbon dioxide recovery system according to sill another aspect is the carbon
dioxide recovery system of [3], in which a pressure of the second distillation column (10) is higher than a pressure of thefirst distillation column (2).
[0053] With this configuration, the compression ratio in the first compressor can be lowered,
so that the overall energy consumption of the carbon dioxide recovery system can be reduced.
[0054] [5] A carbon dioxide recovery system according to still another aspect is the carbon
dioxide recovery system of [3] or [4], including a condensing device (6) for returning a
condensate obtained by cooling an effluent gas from the first distillation column (2) to the first
distillation column (2). The condensing device (6) is provided with a cooler (6e) for cooling
the effluent gas by exchanging heat between the effluent gas and a cooling fluid. The cooling
fluid is at least part of the fluid after the fluid has exchanged heat with the absorption liquid in
the second reboiler (5b).
[0055] With this configuration, since at least part of the fluid after heat exchange with the
absorption liquid in the second reboiler is used to cool the effluent gas from thefirst distillation
column, the thermal efficiency of the entire carbon dioxide recovery system can be improved.
[0056] [6] A carbon dioxide recovery system according to sill another aspect is the carbon
dioxide recovery system of [5], in which the carbon dioxide recovery system is configured such
that the cooling fluid after exchanging heat between the cooling fluid and the effluent gas in the
cooler (6e) is mixed with the fluid from the second distillation column (10) and compressed by
the first compressor (14).
[0057] With this configuration, since the cooling fluid after heat exchange with the effluent
gas in the cooler is supplied to the second reboiler after it is mixed with the fluid from the
second distillation column and compressed by the first compressor, the thermal efficiency of
the entire carbon dioxide recovery system can be improved.
[0058] [7] A carbon dioxide recovery system according to sill another aspect is the carbon
dioxide recovery system of [5], including a second third reboiler (5c) for exchanging heat
between the absorption liquid extracted from the first distillation column (2) and a second fluid;
and a second compressor (30) for compressing the cooling fluid after exchanging heat between
the cooling fluid and the effluent gas in the cooler (6e). The second fluid is the cooling fluid
after being compressed by the second compressor (30).
[0059] With this configuration, since the third reboiler is provided for heating the
absorption liquid by heat exchange between the absorption liquid and the second fluid, the
cooling fluid compressed after heat exchange with the effluent gas in the cooler, the amount of
steam used in the first reboiler is reduced, and the amount of external heat supply to the first
distillation column can be further reduced.
[0060] [8] A carbon dioxide recovery system according to still another aspect is the carbon
dioxide recovery system of [1] or [2], including a third reboiler (5c) for exchanging heat
between the absorption liquid extracted from the first distillation column (2) and a second fluid;
a third compressor (40a, 40b) for supplying a gas obtained by compressing an effluent gas from
the first distillation column (2) to the third reboiler (5c) as the second fluid, and a condensing
device (6) for returning at least part of a condensate obtained by cooling the second fluid after
exchanging heat between the second fluid and the absorption liquid in the third reboiler (5c) to
the first distillation column (2).
[0061] With this configuration, since the third reboiler is provided for heating the
absorption liquid by heat exchange between the absorption liquid and the second fluid, the gas
obtained by compressing the effluent gas from the first distillation column, the amount of steam
used in the first reboiler is reduced, and the amount of external heat supply to the first distillation
column can be further reduced. Additionally, by returning part of the condensate to the
distillation column while discharging the remaining condensate out of the system along with
the drain of the absorption liquid extracted from the first distillation column, the amount of
condensate returned to the first distillation column can be reduced, so that the amount of
external heat supply to the first distillation column can be further reduced.
[0062] [9] A carbon dioxide recovery system according to sill another aspect is the carbon
dioxide recovery system of any one of [1] to [8], in which the fluid is methanol.
Reference Signs List
[0063]
1 Carbon dioxide recovery system
2 First distillation column
5a First reboiler
5b Second reboiler
5c Third reboiler
6 Condensing device
6e Cooler
10 Second distillation column
14 First compressor
30 Second compressor
[0 40a Third compressor
40b Third compressor
. 10 _
Claims (9)
- [Claim1] A carbon dioxide recovery system, comprising:a first distillation column for heating an absorption liquid that has absorbed carbondioxide to release carbon dioxide from the absorption liquid;a first reboiler for exchanging heat between the absorption liquid extracted from the firstdistillation column and steam;a second reboiler for exchanging heat between the absorption liquid extracted from thefirst distillation column and a fluid different from both an effluent gas from the first distillationcolumn and the steam; anda first compressor for compressing the fluid before the fluid flows into the second reboiler.
- [Claim 2] The carbon dioxide recovery system according to claim 1,wherein the fluid includes water, or a hydrocarbon with physical properties of saturationtemperature lower than or equal to 100°C at atmospheric pressure and lower than or equal to120°C at 10 atmospheres, or a hydrocarbon containing oxygen atoms.
- [Claim 3] The carbon dioxide recovery system according to claim 1 or 2, further comprisinga second distillation column different from the first distillation column,wherein the fluid is supplied from the second distillation column.
- [Claim 4] The carbon dioxide recovery system according to claim 3,wherein a pressure of the second distillation column is higher than a pressure of the firstdistillation column.
- [Claim 5] The carbon dioxide recovery system according to claim 3, comprising a condensingdevice for returning a condensate obtained by cooling an effluent gas from the first distillationcolumn to the distillation column, wherein the condensing device is provided with a cooler for cooling the effluent gas by exchanging heat between the effluent gas and a cooling fluid, and wherein the cooling fluid is at least part of the fluid after the fluid has exchanged heat with the absorption liquid in the second reboiler.
- [Claim 6] The carbon dioxide recovery system according to claim 5,wherein the carbon dioxide recovery system is configured such that the cooling fluid afterexchanging heat between the cooling fluid and the effluent gas in the cooler is mixed with thefluid from the second distillation column and compressed by the first compressor.
- [Claim 7] The carbon dioxide recovery system according to claim 5, comprising:a third reboiler for exchanging heat between the absorption liquid extracted from the firstdistillation column and a second fluid; anda second compressor for compressing the cooling fluid after exchanging heat between thecooling fluid and the effluent gas in the cooler,wherein the second fluid is the cooling fluid after being compressed by the secondcompressor.
- [Claim 8] The carbon dioxide recovery system according to claim 1 or 2, comprising:a third reboiler for exchanging heat between the absorption liquid extracted from the firstdistillation column and a second fluid;a third compressor for supplying a gas obtained by compressing an effluent gas from thefirst distillation column to the third reboiler as the second fluid, anda condensing device for returning at least part of a condensate obtained by cooling thesecond fluid after exchanging heat between the second fluid and the absorption liquid in thethird reboiler to the first distillation column.
- [Claim 9] The carbon dioxide recovery system according to claim 1 or 2,- 91i - wherein the fluid is methanol.
Applications Claiming Priority (3)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| JP2021-184701 | 2021-11-12 | ||
| JP2021184701A JP2023072266A (en) | 2021-11-12 | 2021-11-12 | Carbon dioxide recovery system |
| PCT/JP2022/039817 WO2023085086A1 (en) | 2021-11-12 | 2022-10-26 | Carbon dioxide recovery system |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| AU2022385699A1 true AU2022385699A1 (en) | 2024-04-11 |
Family
ID=86335647
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| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| AU2022385699A Pending AU2022385699A1 (en) | 2021-11-12 | 2022-10-26 | Carbon dioxide recovery system |
Country Status (4)
| Country | Link |
|---|---|
| JP (1) | JP2023072266A (en) |
| AU (1) | AU2022385699A1 (en) |
| CA (1) | CA3236450A1 (en) |
| WO (1) | WO2023085086A1 (en) |
Family Cites Families (10)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| JP2003034503A (en) * | 2001-07-19 | 2003-02-07 | Mitsubishi Heavy Ind Ltd | Process for producing synthesis gas and methanol |
| JP4875303B2 (en) * | 2005-02-07 | 2012-02-15 | 三菱重工業株式会社 | Carbon dioxide recovery system, power generation system using the same, and methods thereof |
| JP5641194B2 (en) * | 2010-03-31 | 2014-12-17 | 新日鉄住金エンジニアリング株式会社 | Carbon dioxide gas recovery device |
| JP5707894B2 (en) * | 2010-11-22 | 2015-04-30 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
| JP6064771B2 (en) | 2013-04-26 | 2017-01-25 | 株式会社Ihi | Carbon dioxide recovery method and recovery apparatus |
| JP6307279B2 (en) * | 2014-01-09 | 2018-04-04 | 新日鉄住金エンジニアリング株式会社 | Carbon dioxide gas recovery device and recovery method |
| JP6656843B2 (en) * | 2015-08-21 | 2020-03-04 | 株式会社神戸製鋼所 | Gas processing system and gas processing method |
| KR101709867B1 (en) * | 2015-09-24 | 2017-02-23 | 한국전력공사 | Apparatus for capturing of carbon dioxide |
| JP6938457B2 (en) | 2018-08-08 | 2021-09-22 | キヤノン株式会社 | Transport system, mover, control device and control method |
| JP7356344B2 (en) * | 2019-12-27 | 2023-10-04 | 三菱重工業株式会社 | Boiler plant and carbon dioxide removal method |
-
2021
- 2021-11-12 JP JP2021184701A patent/JP2023072266A/en active Pending
-
2022
- 2022-10-26 CA CA3236450A patent/CA3236450A1/en active Pending
- 2022-10-26 WO PCT/JP2022/039817 patent/WO2023085086A1/en active Application Filing
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| CA3236450A1 (en) | 2023-05-19 |
| JP2023072266A (en) | 2023-05-24 |
| WO2023085086A1 (en) | 2023-05-19 |
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